CN103180678A - Surged heat pump systems - Google Patents

Surged heat pump systems Download PDF

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Publication number
CN103180678A
CN103180678A CN2011800369932A CN201180036993A CN103180678A CN 103180678 A CN103180678 A CN 103180678A CN 2011800369932 A CN2011800369932 A CN 2011800369932A CN 201180036993 A CN201180036993 A CN 201180036993A CN 103180678 A CN103180678 A CN 103180678A
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China
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internal exchanger
cold
temperature
producing medium
evaporimeter
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CN2011800369932A
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CN103180678B (en
Inventor
戴维·怀特曼
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XDX Bbc Worldwide Ltd
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XDX INNOVATIVE REFRIGERATION LLC
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/20—Disposition of valves, e.g. of on-off valves or flow control valves
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B13/00—Compression machines, plants or systems, with reversible cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B30/00—Heat pumps
    • F25B30/02—Heat pumps of the compression type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B47/00—Arrangements for preventing or removing deposits or corrosion, not provided for in another subclass
    • F25B47/006—Arrangements for preventing or removing deposits or corrosion, not provided for in another subclass for preventing frost
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B47/00—Arrangements for preventing or removing deposits or corrosion, not provided for in another subclass
    • F25B47/02—Defrosting cycles
    • F25B47/022—Defrosting cycles hot gas defrosting
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D21/00—Defrosting; Preventing frosting; Removing condensed or defrost water
    • F25D21/04—Preventing the formation of frost or condensate
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D21/00—Defrosting; Preventing frosting; Removing condensed or defrost water
    • F25D21/06—Removing frost
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2313/00—Compression machines, plants or systems with reversible cycle not otherwise provided for
    • F25B2313/027—Compression machines, plants or systems with reversible cycle not otherwise provided for characterised by the reversing means
    • F25B2313/02741—Compression machines, plants or systems with reversible cycle not otherwise provided for characterised by the reversing means using one four-way valve
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/23—Separators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2500/00—Problems to be solved
    • F25B2500/01—Geometry problems, e.g. for reducing size
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2600/00—Control issues
    • F25B2600/25—Control of valves
    • F25B2600/2501—Bypass valves
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2600/00—Control issues
    • F25B2600/25—Control of valves
    • F25B2600/2515—Flow valves
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/30—Expansion means; Dispositions thereof
    • F25B41/385—Dispositions with two or more expansion means arranged in parallel on a refrigerant line leading to the same evaporator

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Other Air-Conditioning Systems (AREA)

Abstract

Surged heat pump systems, devices, and methods are disclosed having refrigerant phase separators that generate at least one surge of vapor phase refrigerant into the inlet of an evaporator during an on cycle of the compressor. This surge of vapor phase refrigerant, having a higher temperature than the liquid phase refrigerant, increases the temperature of the evaporator inlet, thus reducing frost build up in relation to conventional refrigeration systems lacking a surged input of vapor phase refrigerant to the evaporator. The temperature of the vapor phase refrigerant is raised in relation to the liquid phase with heat from the liquid by the phase separation, not by the introduction of energy from another source. The surged heat pump systems may operate in highest heat transfer efficiency mode and/or in one or more higher temperature modes.

Description

Surge formula heat pump
Quoting of related application
The application advocates that the name of submitting on May 27th, 2010 is called the U.S. Provisional Application No.61/348 of " Surged Heat Pump Systems ", 847 priority, and the full content of this application is incorporated into herein by reference.
Background technology
Vapor compression system circulates cold-producing medium in the closed-loop path, so that heat is passed to another foreign medium from a foreign medium.Vapor compression system is used for air conditioning, heat pump and refrigeration system.Fig. 1 represents to come by the compression of cryogenic fluid and expansion traditional steam compression type heat transfer system 100 of work.System 100 is passed to second foreign medium 160 from the first foreign medium 150 along a direction with heat by the closed-loop path.Fluid comprises liquid phase and/or gas phase.Therefore, if the first foreign medium 150 is that room air and the second foreign medium 160 that is contained in a certain structure is this structure air outward, cooling described room air is during operation incited somebody to action by system 100.
Compressor 110 or other compression sets can reduce the volume of cold-producing medium, thereby the poor cold-producing medium that makes of mineralization pressure circulates in the loop.Compressor 110 can be mechanically or the heating power mode reduce the volume of cold-producing medium.Cold-producing medium after compression is then by condenser 120 or heat exchanger, by the surface area between condenser 120 or heat exchanger increase cold-producing medium and the second foreign medium 160.Along with heat is passed to the second foreign medium 160 from cold-producing medium, the volume of cold-producing medium can shrink.
When heat was passed to the cold-producing medium of compression from the first foreign medium 150, the volume of the cold-producing medium of compression can expand.This kind expansion is usually to be realized by metering device 130, and metering device 130 comprises expansion gear and heat exchanger or evaporimeter 140.Evaporimeter 140 can increase the surface area between cold-producing medium and the first foreign medium 150, thereby increases the heat transmission between cold-producing medium and the first foreign medium 150.The transmission of heat from evaporimeter 140 to cold-producing medium can make the phase transformation of at least a portion experience from liquid to gas of the cold-producing medium of expansion.Therefore, can experience temperature with the air of the Surface Contact of evaporimeter 140 reduces.Then, the cold-producing medium after heating is passed and is back to compressor 110 and condenser 120, in compressor 110 and condenser 120, and when heat is passed to the second foreign medium 160, the phase transformation of at least a portion of the cold-producing medium after heating experience from gas to liquid.Therefore, can experience the rising of temperature with the air of the Surface Contact of condenser 120.
Closed-loop path heat transfer system 100 can comprise other elements, for example comprises for connecting the compressor reducer discharge pipe line 115 of compressor 110 with condenser 120.The outlet of condenser 120 can be coupled to condenser discharge pipe line 125, and can be connected to Container, and described Container is used for liquid that the storage liquid level can fluctuate, be used for removing the filter of pollutant and/or drier etc. (not shown).Condenser discharge pipe line 125 can make refrigerant circulation to one or more metering device 130.
Metering device 130 can comprise one or more expansion gear.Metering device 130 comprises the ability of the refrigerant flow that changes this device of flowing through.Expansion gear can be any device that can make the cold-producing medium expansion or the pressure drop of cold-producing medium is measured with the desired speed that operates compatibility with system 100.Therefore, metering device 130 can change the flow of cold-producing medium, and when comprising expansion gear, metering device 130 also comprises the ability that the pressure drop of cold-producing medium is measured.
Metering device 130 can provide static aperture, perhaps can regulate at the duration of work of system 100.Static aperture can be the form of adjustable valve, and described adjustable valve just no longer changes after setting at the duration of work of system 100.Adjustable aperture can have machinery control and electrical control during operation.For example, the machinery that carries out is during operation controlled can or be provided by the fluid that can regulate the barrier film applied pressure in response to the variation of pressure or temperature by bimetallic spring that can adjustment of tonicity.Similarly, the electrical control of carrying out during operation can be provided by servomotor, and the servo-electric function is in response to from the signal of telecommunication of thermocouple and change the aperture.
Have the applicable metering device (being used for the pressure drop of metrology cryogen) that can make the ability that cold-producing medium expands and comprise thermal expansion valve, capillary, fixed and adjustable nozzle, fixed and adjustable aperture, electric expansion valve, automatic expansion valve, hand expansion valve etc.The example of thermal expansion valve comprises Sporlan EBSVE-8-GA (check valve) and the Sporlan RZE-6-GA (two-way valve) that can buy from Parker Han Nifen (Parker Hannifin) company that is positioned at Ohioan Cleveland (Cleveland).Example capillaceous comprises Sporlan F type and Supco BC1-5, and it can be buied from Sa Puke (Supco) company of Alan's Wood (Allenwood) of being positioned at the New Jersey.The example of electric expansion valve comprises the Parker SER6 and 11 that can buy from the Parker Hannifin Corp. that is positioned at Ohioan Cleveland.Also can use other metering devices.
Leave cold-producing medium process swell refrigeration agent transfer system 135 before arriving evaporimeter 140 of the dilation of metering device 130, swell refrigeration agent transfer system 135 can comprise one or more cold-producing medium guider 136.For example when the position of metering device 130 near evaporimeter 140 or when combining with evaporimeter 140, swell refrigeration agent transfer system 135 can combine with metering device 130.Therefore, the bulge of metering device 130 can be connected to one or more evaporimeter by swell refrigeration agent transfer system 135, and swell refrigeration agent transfer system 135 can be single pipe or comprises a plurality of elements.For example, as in U.S. Patent No. 6,751,970 and No.6, described in 857,281, metering device 130 and swell refrigeration agent transfer system 135 can have element still less or also have other elements.
One or more cold-producing medium guider 136 can combine with metering device 130, swell refrigeration agent transfer system 135 and/or evaporimeter 140.Therefore, the function of metering device 130 can be divided between one or more expansion gear and one or more cold-producing medium guider, and can and deposit, separate or combine with swell refrigeration agent transfer system 135 and/or evaporimeter 140.Applicable cold-producing medium guider comprises pipe, nozzle, fixed and adjustable aperture, distributor, a series of distributor tube, direction change valve etc.
Evaporimeter 140 receives the cold-producing medium that is essentially liquid and has the expansion of a small amount of steam minute rate (vapor fraction), and makes heat be passed to the cold-producing medium of expansion from the first foreign medium 150 that is positioned at closed-loop path heat transfer system 100 outsides.Therefore, evaporimeter or heat exchanger 140 impel heat (for example air of environment temperature) move to second source (for example expand cold-producing medium) from a source.Suitable heat exchanger can be taked various ways, comprises copper pipe, plate and frame (plate and frame), shell-and-tube (shell and tube), cold wall (cold wall) etc.Many traditional systems are designed and are operable at least in theory at the interior cold-producing medium that the liquid part of cold-producing medium is converted fully to evaporation of evaporimeter 140.Comprise the heat transfer that liquid refrigerant is transformed into gas phase, it is overheated that the cold-producing medium of evaporation also becomes, thereby have over the temperature of the boiling point of cold-producing medium and/or increase the pressure of cold-producing medium.Cold-producing medium leaves evaporimeter 140 and is back to compressor 110 by evaporimeter discharge pipe line 145.
In traditional vapor compression system, the cold-producing medium of expansion enters evaporimeter 140 with the obvious temperature lower than the temperature of evaporimeter surrounding air.Along with heat is passed to cold-producing medium from evaporimeter 140, refrigerant temperature is increased to the temperature higher than evaporimeter 140 surrounding airs in the follow-up or downstream part of evaporimeter 140.This kind between the initial or intake section of evaporimeter 140 and the follow-up or exit portion of evaporimeter 140 quite significantly temperature difference can cause oil to be detained and the frosting problem at intake section.
Fig. 2 A and Fig. 2 B represent to have the conventional heat pump system 200 of the ability of conducting heat along both direction.Therefore, system 100 can be passed to the second foreign medium 160 from the first foreign medium 150 with heat, maybe heat can be passed to the first foreign medium 250 (Fig. 2 B) from the second foreign medium 260 and heat pump 200 can be passed to the second foreign medium 260 (Fig. 2 A) from the first foreign medium 250 with heat.By this kind mode, can think that the heat-transfer capability of system 200 is " can be reverse ".
In the conventional heat pump embodiment, internal exchanger 240 is placed in is conditioned the space, simultaneously external heat exchanger 220 is placed in (normally outdoor) outside the space that is conditioned.Be conditioned the inside that the space can be room, automobile, refrigerator, cooler, freezer etc.
System with heat from being conditioned the space is passed to outdoor refrigeration mode, internal exchanger 240 is as evaporimeter, and external heat exchanger 220 is as condenser.Otherwise, in system, heat being passed to from outdoor the heat pump mode that is conditioned the space, internal exchanger 240 is as condenser, and external heat exchanger 220 items is as evaporimeter.Therefore, at all events planting mode of operation, is all that heat is passed to evaporimeter from condenser all the time.
Be different from one-way fashion system 100, reversible heat pump 200 utilizes 280 and two metering devices 230,233 of flow inversion device (flow reverser), thereby can transmit cold-producing medium on either direction.When compressor 210 transmits cold-producing medium in one direction, flow inversion device 280 allows internal exchanger 240 or external heat exchanger 220 to present to evaporimeter discharge pipe line 245, and 245 low-pressure inlet sides to compressor 210 of evaporimeter discharge pipe line are presented.Therefore, flow inversion device 280 switches system between heating the first foreign medium 250 or cooling the first foreign medium 250.The example of flow inversion device comprises Ranco V2 and the V6 product that can buy from gloomy Ying Weisi (Invensys) company of stepping on Portland building (Portland House, Bressenden Place) of the mine-laying that is positioned at London.Also can use other flow inversion devices.
At any one time, one of them metering device is used for making cold-producing medium expand and/or the pressure drop of cold-producing medium is measured, and the second metering device makes back flow of refrigerant and is not used in cold-producing medium is expanded.Therefore, remove heat with the cooling Fig. 2 A that is conditioned the space from the first foreign medium 250 therein, metering device 230 expands cold-producing medium, and metering device 233 makes back flow of refrigerant.Similarly, provide from the second foreign medium 260 at heat to be conditioned the space with Fig. 2 B that heats the first foreign medium 250, metering device 233 expands cold-producing medium, metering device 230 makes back flow of refrigerant.
If any one in metering device 230,233 be not two-way and thereby do not have the back flow of refrigerant of making and keep the ability of desired properties, as shown in Fig. 2 C (refrigeration) and Fig. 3 D (heating), can with the one-way fashion metering device with comprise one-way fashion check-valves 270,273 bypass circulation 271,272 is combined with.Therefore, when a metering device expanded cold-producing medium, bypass circulation and check-valves made the second metering device by bypass.Check-valves can prevent that cold-producing medium from refluxing by the one-way fashion metering device that is associated.
The shortcoming of conventional heat pump is, because it has two kinds of functions (the same space that is conditioned is heated and freezes), thereby it is not to be optimized for any in these two kinds of functions.Heat pump 200 shown in Fig. 2 B provides a kind of mode of heat in internal exchanger 240 be to provide restriction to cold-producing medium stream in swell refrigeration agent transfer system 235.Although this kind restriction can be arranged in the optional position of swell refrigeration agent transfer system 235 and all system appropriately worked, yet described restriction is usually incorporated in one or more cold-producing medium guider 236.If make cold-producing medium guider 236 less than the best for refrigeration, cold-producing medium can reach higher temperature and pressure in internal exchanger 240 during heating, and this is because cold-producing medium more is difficult to discharge internal exchanger 240.Therefore, although system 200 can provide heat to the interior space, yet the refrigerating efficiency that system provides significantly reduce, this is because described restriction also can limit cold-producing medium and enters internal exchanger 240 during freezing.
Not only because making compressor 210 waste energy with higher pressure work when originally obtaining best refrigerating efficiency, because compressor 210 will carry out work for described restriction when heating and freeze, thereby with respect to wherein compressor 210 is when heating but not for the system that working strength is larger when freezing, the working life of compressor 210 shortens.
Although heat pump is for general in temperate climate and heats being conditioned the space, yet heat pump also can be used for colder area, for example in the time electric power can only being provided and wanting to use resistance coil to heat.Colder area is that the average low temperature in winter is about 0 ℃ and following area.Colder area is that the average low temperature in winter is about-7 ℃ and following area.From approximately 0 ℃ when beginning to reduce, the utilization rate of heat pump significantly descends when the average low temperature in winter.For example, perishing area (for example middle part, northeast, middle part, northwest and mountain area) in the U.S., the utilization rate of heat pump in newer single resident family is lower than 10%, and in warmer South Atlantic Ocean, middle part, the southeast and southwestern middle part, the heat pump utilization rate on average is about 47%.
Although heat pump can use in these colder areas, if basically do not melt in closing the cycle yet accumulate in frost on external heat exchanger 220 in the connection cycle of compressor 210 (heating), may need to carry out defrosting cycle and defrost and make system 200 recover heat transfer efficiencys.Along with heat is passed to internal exchanger 240 and the temperature of external heat exchanger 220 is descended, external heat exchanger 220 is from outdoor extraction heat, make surface temperature be maintained at that more than 0 ℃, the ability with preventing frosting can reduce with the decline of outside air temperature simultaneously.
Therefore, external heat exchanger 220 is as in the heating mode of evaporimeter therein, and the frosting of external heat exchanger 220 can become significant problem because needs defrost continually.The reason of this kind frosting usually is: the cold-producing medium of the expansion in the start-up portion of external heat exchanger 220 is in the temperature lower than the dew point of extraneous air, thereby causes heating the duration of work moisture condensation and freezing on external heat exchanger 220.Therefore, as the indoor evaporator that is used for refrigeration, the external heat exchanger 220 of heat pump can be frozen during heating.In fact, for the external heat exchanger of heat pump, this problem can be even more serious, and this is because system is conditioned the air themperature in space can't obviously change the moisture content of extraneous air and the outside air temperature when heating generally lower than refrigeration the time.
Because frost during heating can surround the part on the surface of external heat exchanger, thereby the surface of the frosting direct contact chamber outer air of coil pipe that makes external heat exchanger 220.As a result, on external heat exchanger 220 and/or the air stream that passes external heat exchanger 220 reduces and external heat exchanger 220 descends from the ability (heating efficiency) of outdoor absorption heat.Therefore, for the energy that consumes, heat pump 200 can reduce (heating efficiency decline) from outdoor amount to being conditioned the heat that transmits in the space, and system 200 can also descend from outdoor speed to being conditioned the space transferring heat.The temperature that the decline of this kind heat transfer efficiency causes being provided to the heated air that is conditioned the space descends.
The conventional heat pump system can defrost passively by close compressor 210, perhaps can be by 220 heating defrost on one's own initiative to external heat exchanger in defrosting cycle.No matter use a kind of in these two kinds of methods or two kinds, if defrosting all requires to use not need to suspend with system to compare larger vapor compression system when desired heat direction of transfer defrosts.
When compressor 210 disconnects during passive defrosting, the rate reduction that system 200 can heat being conditioned the space.Can control passive defrosting cycle by simple timing mechanism, for example when compressor 210 keep connecting reach the selected period 30% the time, regardless of the amount that is conditioned the required heat in space, all carry out passive defrosting cycle.Also can control passive defrosting cycle by electronic circuit, the performance of described electronic circuit monitoring external heat exchanger 220, and try hard to for the efficient of losing because external heat exchanger 220 is defrosted, the work of compressor 210 be maximized.
For active defrosting, generally by system 200 is passed to the heat transmission that is conditioned the space and is back to external heat exchanger 220 from outdoor before this, heat is passed to external heat exchanger 220 from being conditioned the space.Therefore, when external heat exchanger 220 is carried out initiatively defrosting, heat although be conditioned space requirement, yet heat pump is with refrigeration mode work, and consumed energy with heat is moved back to its from outdoor.In addition, blown over internal exchanger 240 when preventing that internal exchanger 240 from freezing from the heated air that is conditioned the space during defrosting initiatively, can provide additional heat to prevent that locking system provides cold air to being conditioned the space by induction coil or other devices.Therefore, need the conventional heat pump system of frequent defrosting to come work as being forced to the air inductive heater, it also must heating external heat exchanger 220 except heating is conditioned the space.This can make because gaining and incur loss to being conditioned the conduct heat any theoretical energy efficiency obtains of space from outdoor.
Therefore, need a kind of heat pump that has the efficient of raising when freezing and heating badly.Wish that also heat pump is during heating, especially more can overcome the external heat exchanger frosting in colder area.System disclosed in this invention, method and device have overcome at least one shortcoming in the shortcoming that joins with the conventional heat pump System Dependent.
Summary of the invention
A kind of heat pump of the present invention has phase separator, and described phase separator is providing one or more surge of the gas phase of cold-producing medium to enter evaporimeter when being conditioned the space transferring heat.The surge of gas phase has the temperature higher than the liquid phase of cold-producing medium, thereby evaporimeter is heated to defrost.Described system can comprise the Flow-rate adjustment member, to heat duration of work help generation frictional heat.
A kind of heat pump of the present invention has at least two phase separators, to being conditioned the space transferring heat or during be conditioned the space transferring heat, described two phase separators provide one or more surge of the gas phase of cold-producing medium to enter to be positioned at the evaporimeter that is conditioned the space and to be positioned at the evaporimeter that is conditioned outside the space.The surge of gas phase has the temperature higher than the liquid phase of cold-producing medium, thus heat in these two evaporimeters any one defrost.Described system can comprise the Flow-rate adjustment member, to heat duration of work help generation frictional heat.But operating said system comprises liquid phase or does not comprise liquid phase so that leave the cold-producing medium that is positioned at the evaporimeter outside the living space.
Description of drawings
With reference to the following drawings and explanation, can understand better the present invention.Each element in accompanying drawing may not be drawn in proportion, but focuses on illustration principle of the present invention.
Fig. 1 represents the schematic diagram according to traditional steam compressed heat transfer system of prior art.
Fig. 2 A represents to comprise that the conventional heat pump system of reversible metering device provides the schematic diagram of refrigeration to being conditioned the space.
Fig. 2 B represents to comprise that the conventional heat pump system of reversible metering device provides to being conditioned the space schematic diagram that heats.
Fig. 2 C represents to comprise that the conventional heat pump system of bypass circulation and one-way fashion valve provides the schematic diagram of refrigeration to being conditioned the space.
Fig. 2 D represents to comprise that the conventional heat pump system of bypass circulation and one-way fashion valve provides to being conditioned the space schematic diagram that heats.
Fig. 3 A represents that the surge formula internal exchanger heat pump that comprises the Flow-rate adjustment member provides the schematic diagram of refrigeration to being conditioned the space.
Fig. 3 B represents that the surge formula internal exchanger heat pump that comprises the Flow-rate adjustment member provides to being conditioned the space schematic diagram that heats.
Heat pump shown in Fig. 4 A presentation graphs 3A is at the schematic diagram that is modified to when having phase separator, and described phase separator can provide cold-producing medium to external heat exchanger during freezing.
Heat pump shown in Fig. 4 B presentation graphs 3B is at the schematic diagram that is modified to when having phase separator, and described phase separator can provide cold-producing medium to external heat exchanger during heating.
Fig. 5 A is illustrated in to have the surge formula refrigeration that independent complete surge loop and local wave regurgitate the road during refrigeration and heats heat pump.
Have the surge formula refrigeration that independent complete surge loop and local wave regurgitate the road during Fig. 5 B is illustrated in and heats and heat heat pump.
Fig. 6 represents a kind of flow chart that operates the method for heat pump.
Fig. 7 represents a kind of flow chart of the method that in heat pump, evaporimeter is defrosted.
Fig. 8 represents a kind of phase separator to be arranged bypass with the flow chart of the method for carrying out heating operation.
The specific embodiment
Surge formula vapor compression heat pump system comprises the cold-producing medium phase separator, and described cold-producing medium phase separator enters in the entrance of evaporimeter for generation of at least one surge of vapor phase refrigerant.Evaporimeter can be positioned at and be conditioned space or outdoor.Described surge produces by operating phase separator with refrigerant mass fluxes (mass flow rate), and described refrigerant mass fluxes can be decided according to the design of phase separator and the heat transfer capacity of size and cold-producing medium.Described one or more surge can produce during the connection cycle of compressor.
The surge of vapor phase refrigerant can have the temperature higher than liquid phase refrigerant.With respect to the initial temperature of the cold-producing medium of the expansion that is supplied to phase separator, the liquid that obtains from phase separator will be cooler and the steam that obtains from phase separator with the initial temperature of heat in the cold-producing medium that expands.Therefore, the temperature of steam is the heat by being derived from liquid when being separated but not obtains raising by introducing energy from another source.
Can the raise temperature of initial or intake section of evaporimeter of surge, thus carry out can reducing gathering of frost for the conventional heat pump system of surge input with respect to not existing to the vapor phase refrigerant of evaporimeter.For for the heating of cool region, reducing gathering of frost can be especially favourable, and this is because can reduce or no longer need to use extra heat (for example from compressor, heater coil etc.) to defrost.
By setting up bypass to being used for to the phase separator that internal exchanger is presented, described system can provide high heat transfer efficiency during freezing, provide heat to being conditioned the space simultaneously during heating.By to being conditioned the space and to the outdoor surge formula evaporator operation that provides, can being increased to and being conditioned the space and from being conditioned the heat transfer efficiency in space.By provide independent complete and local wave to regurgitate the road for external heat exchanger, described system can provide high heat transfer efficiency pattern and higher temperature pattern, reduces simultaneously during heating the needs at compressor place's rising refrigerant pressure.
In Fig. 3 A and Fig. 3 B, phase separator 331 and Flow-rate adjustment member 332 are integrated into respectively in the conventional heat pump system shown in Fig. 2 C and Fig. 2 D, so that surge formula refrigeration heat pump system 300 to be provided.Fig. 3 A is expressed as and is conditioned the system 300 that the space provides refrigeration, and Fig. 3 B is expressed as and is conditioned the space system 300 that heats is provided.
System 300 comprises compressor 310, external heat exchanger 320, metering device 330,333 and internal exchanger 340.When compressor 310 transmitted cold-producing medium along a direction, flow inversion device 380 allowed internal exchanger 340 or external heat exchanger 320 to present to evaporimeter pipeline 345, and 345 low-pressure inlet sides to compressor 310 of evaporimeter pipeline are presented.Flow-rate adjustment member 332 can be placed in the bypass circulation 371 between one way stop peturn valve 370 and phase separator 331.When internal exchanger 340 was used as condenser in heating mode, the Flow-rate adjustment member can provide to the cold-producing medium that leaves internal exchanger 340 required restriction.When indoor heat exchanger 340 was used as evaporimeter in refrigeration mode, phase separator 331 was presented to indoor heat exchanger 340.If metering device 333 does not allow the cold-producing medium two-way flow, can use 373 pairs of metering devices of optional bypass circulation 372 and optional one way stop peturn valve 333 to carry out bypass.Therefore, the exterior section of system 300 can be configured to as the front with reference to Fig. 2 C and the described legacy system 200 or 201 of Fig. 2 D.Surge formula refrigeration heat pump system 300 can have element still less or also have extra element.
Phase separator 331 can be integrated mutually or separate with metering device 330 with metering device 330.When separating with metering device 330, phase separator can comprise the Flow-rate adjustment member, so that come the cold-producing medium stream of automatic measurer 330 to be adapted to phase separator 331.After phase separator 331 can be integrated in the dilation of metering device 330 and before internal exchanger 340.Phase separator 331 can be by integrating with any mode and the metering device 330 of the required running parameter compatibility of system.Before phase separator 331 is positioned at the entrance of internal exchanger 340 or porch.Can between phase separator 331 and internal exchanger 340, other elements be set, fixed or adjustable nozzle, refrigerant distributor, refrigerant distributor feed line for example be set, be used for changing heat exchanger and one or more valve of refrigerant condition.Yet, these other elements preferably be configured to basically not can EVAC 300 the surge operation.Metering device 330 and phase separator 331 can have element still less or also have other elements.
Phase separator 331 comprises body, and described body defines separator inlet, separator outlet and refrigerant storage chambers.Entrance and outlet can be aligned to and make angle is approximately 40 ℃～approximately 110 ℃.The longitudinal size of described chamber can be parallel to separator outlet; Yet, also can use other structures.Described longitudinal size can be approximately 4 times～5.5 times and approximately 6 times～approximately 8.5 times of separator inlet diameter of separator outlet diameter.The locker room has the volume that is defined by longitudinal size and chamber diameter.
Phase separator 331 is used for entering heat exchanger (for example internal exchanger 340) at cold-producing medium makes the liquid of cold-producing medium of the expansion of automatic measurer 330 to separate at least in part with steam before.The design and the size that comprise phase separator 331, the separation of liquid phase and gas phase also can be affected by other factors, and these factors comprise the running parameter of compressor 310, metering device 330, swell refrigeration agent transfer system 335, other pumps, flux enhancement device (flow enhancer), flow restrictor (flow restrictor) etc.
Can provide the vapor phase refrigerant surge for the start-up portion of internal exchanger 340 by be equipped with phase separators for system 300, the separator inlet diameter of described separator is approximately 1: 1.4～4.3 or approximately 1: 1.4～2.1 to the ratio of separator outlet diameter; The separator inlet diameter is approximately 1: 7～13 to the ratio of separator longitudinal size; And the separator inlet diameter is approximately 1: 1～12 to the ratio of refrigerant mass fluxes.Although these ratios are take centimetre as long measure, represent take kg/hr as mass flow unit, yet also can use other ratios, comprise the ratio that adopts other long measures and mass flow unit.
Between the separation period of the cold-producing medium that expands, the clean heating of the clean cooling and steam of liquid can occur.Therefore, initial temperature with respect to the cold-producing medium of the expansion that is supplied to phase separator 331, the liquid that obtains from phase separator 331 will be cooler than the initial temperature of the cold-producing medium of expansion, and the steam that obtains from phase separator 331 is with the initial temperature of heat in the cold-producing medium that expands.Therefore, steam temperature be by when being separated from the heat of liquid but not raise by introducing energy from another source.By this kind mode, to being conditioned to conduct heat in the space or during be conditioned the space and conduct heat, can utilizing phase separator 331 to reduce or eliminate during active defrosting and introduce by the refrigerant vapour of another source (for example compressor, heater coil etc.) heating or the needs of liquid to evaporimeter.
During surge, the temperature of the start-up portion of internal exchanger 340 can be increased to than below the low approximately temperature of 1 ℃ of environment temperature.In addition, during surge, the start-up portion of internal exchanger 340 can become heat in the dew point of heat exchanger surrounding air on every side.During this external surge, at least 0.5 ℃ of the dew point height of the comparable heat exchanger ambient air of the cold-producing medium in the start-up portion of internal exchanger 340 or may be up to few 2 ℃.
By phase separator 331 work are introduced in evaporimeter (for example internal exchanger 340 of Fig. 3 A) with the surge with cold-producing medium, so that surge formula refrigeration heat pump system 300 to be provided, wherein said surge is steam between each work period of introducing cold-producing medium to evaporimeter basically, and described evaporimeter comprises the liquid component with respect to steam surge showed increased.System 300 provides the speed of cold-producing medium to obtain duration of work preferred steam surge frequency for specific heat transfer applications at compressor 310 according to the design of phase separator 331 and size and to phase separator 331.
The phase separator inlet diameter can increase or reduce with respect to these rate values the ratio of phase separator longitudinal size, until till system 300 no longer provides required surge rate.Therefore, by changing the separator inlet diameter to the ratio of longitudinal size, can change the surge frequency of system 300, until till system 300 no longer provides required surge effect.According to its dependent variable, can increase or reduce the separator inlet diameter to these rate values of refrigerant mass fluxes, until till surge stops.Can increase or reduce the separator inlet diameter to these rate values of refrigerant mass fluxes, until surge stops or required refrigeration no longer is provided till.Those of ordinary skill in the field can determine that other rate values provide a required surge or a plurality of surge, required surge frequency, refrigeration or its combination etc.
The liquid of the cold-producing medium by separating at least in part described expansion before introducing evaporator inlet at the cold-producing medium that will expand and steam and by make vaporous cryogen basically surge enter evaporimeter, system 300 produces temperature fluctuation in the start-up portion of evaporimeter.The start-up portion of evaporimeter or intake section can be the most close entrance the evaporimeter volume front 30%.The start-up portion of evaporimeter or intake section can be the most close entrance the evaporimeter volume front 20%.Also can use other intake sections of evaporimeter.The start-up portion of evaporimeter of experience temperature fluctuation or intake section can be at the most approximately 10% of evaporimeter volume.Can make system 300 work to prevent or basically eliminate in evaporimeter in the start-up portion of evaporimeter or the temperature fluctuation in response to the steam surge after intake section.In the situation that the refrigeration capacity of no liquid, the steam surge makes the temperature of the start-up portion of evaporimeter present the forward fluctuation.
When system 300 works with refrigeration mode as shown in Figure 3A, provide to the surge that is essentially steam of the start-up portion of internal exchanger 340 and can be at least 50% steam (vaporous cryogen quality/liquid refrigerant quality).Also can make 300 work of surge formula system provide the surge of the refrigerant vapour with at least 75% or at least 90% steam with the start-up portion to internal exchanger 340.These surges can make peak temperature at intermittence that the start-up portion of evaporimeter reaches be in below the low approximately temperature of 5 ℃ of temperature than the first foreign medium 350.The peak temperature at intermittence that the start-up portion of evaporimeter reaches also can be in than below the low approximately temperature of 2.5 ℃ of the temperature of the first foreign medium 350.These intermittently peak temperature preferably higher than the dew point that is conditioned the air in the space.Also can reach other intermittently peak temperatures.
When with the work of as shown in Figure 3A refrigeration mode, surge formula refrigeration heat pump system 300 also can be worked provides approximately 1.9Kcal with the start-up portion of heat exchanger 340 internally to exit portion thh -1m -2℃ -1～about 4.4Kcal thh -1m -2℃ -1Mean heat transfer coefficient.Mean heat transfer coefficient is by measuring heat transfer coefficients and the coefficient of gained is averaged to determine at the starting point of heat exchanger internally at least 5 some places to terminal.System 300 this heat transfer property during freezing significantly improves with respect to the non-surge formula of tradition refrigeration heat pump system, wherein, in the non-surge formula of tradition refrigeration heat pump system, the start-up portion of internal exchanger has in the initial part office of internal exchanger coil pipe lower than about 1.9Kcal thh -1m -2℃ -1Heat transfer coefficient, the internal exchanger part before outlet in have lower than about 0.5Kcal thh -1m -2℃ -1Heat transfer coefficient.
The mean temperature that comprises the start-up portion of evaporimeter when making compressor 310 work for the conventional heat pump system raises, the start-up portion of the evaporimeter of system 300 also experiences intermittently peak temperature in response to the steam surge, peak temperature can approach and be equal to or higher than foreign medium (for example evaporimeter ambient air) described intermittence.The peak temperature at intermittence that the start-up portion of evaporimeter experiences can reduce the trend of this part frosting of evaporimeter.Intermittently peak temperature also can make at least a portion thawing or the distillation that is formed at any frost on the evaporimeter start-up portion at compressor 310 duration of works, thereby defrosts from evaporimeter.
Can affect in fact the start-up portion of the internal exchanger 340 of most possible frosting due to the intermittent temperature rising that causes because of the steam surge, thereby with respect to the conventional heat pump system, the average operating temperature of whole internal exchanger 340 can reduce in refrigeration mode, and can not increase the tendency of the start-up portion frosting of internal exchanger 340.Therefore, with respect to traditional heat pump, no matter surge formula heat pump 300 is do not work or pass through to the active method of evaporimeter 340 introducing heats by 310 long periods of compressor, can reduce the needs of defrosting, simultaneously can also be from realize the raising of refrigerating efficiency than the harmonic(-)mean temperature in whole internal exchanger 340.
Comprise the benefit that the batch temperature of the initial part office of evaporimeter raises, phase separator 331 made cold-producing medium before cold-producing medium is introduced evaporimeter steam part and the ability that the liquid part is separated at least in part provide other advantage.For example, the conventional heat pump system that separates at least in part with the steam part that does not make cold-producing medium before cold-producing medium during freezing is introduced into evaporimeter and liquid part compares, and when compressor 310 work, system 300 can experience higher pressure in evaporimeter.Because the volume of the cold-producing medium in evaporimeter is greater than the volume in the conventional heat pump system, these the higher pressure in evaporimeter can strengthen the heat transfer efficiency of system 300.This increase of evaporimeter (internal exchanger 340) operating pressure also makes the compression ratio during refrigeration lower, thereby realizes minimizing and system element life-time dilatation that energy consumes.
The conventional heat pump system that separates at least in part with the steam part that did not make cold-producing medium before being introduced into evaporimeter and liquid part compares, separate at least in part with the liquid part by the steam part that made cold-producing medium before being introduced into evaporimeter, not only can improve evaporator pressure, also can improve the flow through mass velocity of evaporimeter of cold-producing medium.In evaporimeter, higher refrigerant quality speed can be the heat transfer efficiency that surge formula refrigeration heat pump system 300 provides enhancing, and this is because with respect to the conventional heat pump system, more cold-producing medium is arranged through evaporimeter in preset time.
Made steam part and the liquid part of cold-producing medium separate at least in part the temperature reduction of the liquid part that also can make cold-producing medium before being introduced into evaporimeter.This kind reduction can make the liquid part of cold-producing medium partly have larger refrigeration capacity than steam, thereby the total amount of heat that the cold-producing medium through evaporimeter is transmitted increases.By this kind mode, the cold-producing medium of the equal in quality of process evaporimeter can absorb more heat than conventional heat pump system during freezing.
The cold-producing medium that the steam part that made cold-producing medium before being introduced into evaporimeter and the ability that the liquid part is separated at least in part also can make the evaporator outlet place partly but not bone dry.Therefore, be introduced into steam part and the liquid parameter partly of the cold-producing medium of evaporimeter by adjusting, a small amount of liquid part can reside in the cold-producing medium that leaves evaporimeter.By keep the liquid part of cold-producing medium in whole evaporimeter, can improve the heat transfer efficiency of system.This kind reduction of evaporimeter (internal exchanger 340) temperature also can make the thermal pressure that condenser (external heat exchanger 320) is located during refrigeration reduce, thereby realizes minimizing and the system element life-time dilatation that energy consumes.Therefore, system compares with conventional heat pump, and the evaporimeter of same size (internal exchanger) can be from being conditioned the space to the more heats of outdoor transmission.
The steam part of cold-producing medium is separated at least in part with the liquid part also can obtain enough refrigerant quality speed, liquid refrigerant is covered on the inner periphery of pipeline of the cold-producing medium guider 236, cold-producing medium transfer system and/or the evaporimeter start-up portion that form the metering device back being enough to.When occuring, the total refrigerant quality in the start-up portion of evaporimeter is from about 30%～approximately 95% steam (mass/mass).If lose, the liquid of circumference is covered, when the vapor/liquid ratio that returns to approximately 30%～approximately 95%, will recover to cover.In this way, compare with the conventional heat pump system that lacks phase separator after in when refrigeration that liquid covers, can make the heat transfer efficiency raising of the initial part office of evaporimeter.Thereby about using phase separator to provide more discussing in detail of surge operation cooled interior space to be found in that on May 15th, 2009 submitted to inner evaporator and name is called the international application case No.PCT/US09/44112 of " Surged Vapor Compression Heat Transfer System with Reduced Defrost ", the full content of this application is incorporated into by reference.
For the phase separator 331 that these benefits are provided during freezing, the additional limits that the swell refrigeration agent transfer system 335 of conventional heat pump system is increased is not basically disturbed and is separated and caused surge formula evaporator operation.Therefore, when being conditioned the space and freezing for the benefit of surge operation is provided, can not use traditional restriction, for example use the cold-producing medium guider 336 less than stock size.The benefit that obtains from the operation of the surge of indoor heat exchanger 340 for (Fig. 3 A) during remaining on refrigeration, can carry out bypass with bypass circulation 371, one way stop peturn valve 370 and 332 pairs of phase separators of Flow-rate adjustment member 331 during heating, thereby the increase of refrigerant pressure expectation in internal exchanger 340 (Fig. 3 B) is provided.In this way, Flow-rate adjustment member 332 applies restriction to the cold-producing medium that leaves internal exchanger 340 during heating, and described being limited in do not disturbed cold-producing medium stream during refrigeration basically.Thereby, can be heating performance the cold-producing medium that flows out from indoor heat exchanger 340 is selected suitable restriction, and need not consider the reduction of the refrigeration performance that script may occur.
As U.S. Patent No. 6,401, described in 470, No.6,401,470, No.6,857,281, No.6,915,648 etc., although do not require to have controllability, Flow-rate adjustment member 332 preferably can be regulated.The Flow-rate adjustment member also can electric means or mechanical system controlled, on one's own initiative heat pump 300 is carried out required restrictions heating duration of work.If controlled, can increase restriction, with the temperature of the internal exchanger 340 that raises in response to extraneous air, the air that enters internal exchanger 340, the air that leaves internal exchanger 340, the temperature that is back to the air etc. of internal exchanger 340.On the contrary; also can reduce the restriction that is provided by the controlled flow adjustment means, with protection compressor 310 or in response to the ampere of the temperature of compressor 310, compressor 310 consume, line pressure between compressor 310 and internal exchanger 340 etc. and energization efficient.
Separate although one way stop peturn valve 370 and Flow-rate adjustment member 332 are expressed as in Fig. 3 A and Fig. 3 B, also can integrate with in a shell etc.Although as shown in Fig. 3 A and Fig. 3 B, Flow-rate adjustment member 332 is positioned at the right side of one way stop peturn valve 370, but any position that Flow-rate adjustment member 332 does not disturb the work of phase separator 331 can be incorporated in refrigeration in the high pressure line of Fig. 3 B (heating) during basically yet comprises on the either side that is positioned at one way stop peturn valve 370.
The example that can be in system 300 be used for preventing the one way stop peturn valve that cold-producing medium refluxes by phase separator 331 comprises the Parker274037-12 that can buy from Parker Han Nifen (Parker Hannifin) company and the Superior900MA-10S that can buy from the Si Bier valve company (Superior Valve Co.) of the Houston that is positioned at Texas.Comprise the device of selling as check-valves, also can use compatible with the work of system and can prevent basically that cold-producing medium from passing through any device that phase separator 331 refluxes.For example, can use the switching mode magnetic valve that is subjected to electrical control or in response to the valve of pressure reduction.Because cold-producing medium will be along the path of minimum drag by the pipeline of heat pump, so also can make cold-producing medium replace check-valves by the more disadvantageous device of the backflow of phase separator 331 with comparing with desired path.
In Fig. 4 A and Fig. 4 B, the surge formula refrigeration heat pump system 300 of Fig. 3 A and Fig. 3 B is modified to respectively has phase separator 434, phase separator 434 provides cold-producing medium to external heat exchanger 420 during heating, thereby surge formula refrigeration is provided and heats heat pump 400.Although being expressed as, system 400 has one way stop peturn valve 473 and bypass circulation 472, if flow along reciprocal cold-producing medium but metering device 433 can provide two-way flow and phase separator 434 to be configured to not appreciable impact, one way stop peturn valve 473 and bypass circulation 472 these elements are also non-essential.Thereby system 400 provides the operation of surge formula for the arbitrary heat exchanger as evaporimeter.System 400 can have element still less or also have extra element.
For example, although system 400 is expressed as has the phase separator of both presenting to internal exchanger 440 and external heat exchanger 420, but also can omit the phase separator of presenting to internal exchanger 440, thereby provide the surge formula to heat heat pump, although the associated loss on refrigerating efficiency is arranged.Although also being expressed as, system 400 has Flow-rate adjustment member 432 to provide required restriction to swell refrigeration agent transfer system 435 during heating, if but the heating efficiency that obtains from the operation of the surge of evaporimeter (external heat exchanger 420) during heating can provide required heat to being conditioned the space, Flow-rate adjustment member 432 also can omit.
Comprise at the same time in the system 400 of two phase separators, all strengthen on two heat transfer directions thereby evaporimeter absorbs the ability of heat effectively with surge formula work pattern.The system 400 of Fig. 4 A and Fig. 4 B not only has before in conjunction with the system 300 of Fig. 3 A and Fig. 3 B is described and is arranged in refrigeration benefit when being conditioned the space when evaporimeter, also has to make to be positioned at outdoor evaporimeter also to have the benefit that previous described surge formula operates during heating.Thereby system 400 provides increases the benefit of conducting heat, and has also reduced not only internal exchanger 440 during the refrigeration, also the external heat exchanger 420 during heat is carried out passive and/or the benefit of the demand of defrosting initiatively.
During heating, the needs of evaporimeter (external heat exchanger 460) defrosting are reduced in that colder area especially expects, this is to make system 400 more heat can be sent to be conditioned the space because can operate the ability of the entrance of external heat exchanger 420 under higher mean temperature when absorbing identical or more substantial heat from outdoor air.Thereby, during heating to the temperature in external heat exchanger 420 exits measure will represent cold-producing medium the surge trace of operating period (such as before for the system 300 during refrigeration discussion).By using sensor 421 externally exit monitor temperature and/or the pressure of heat exchanger 420, adjustable metered device 433 is with the externally interior maintenance surge operation of heat exchanger 420.Thereby, when system 400 is used for average outdoor temperature and can causes excessive frosting and/or the active defrosting cycle more too much than legacy system needs colder regional originally, system's 400 needs defrosting cycle still less.Surge formula evaporator operation during heating makes system 400 to be arranged on and can't use in the colder area of conventional heat pump system.
When system 400 worked with heating mode as shown in Fig. 4 B, the surge that is essentially steam of the cold-producing medium that provides to the start-up portion of external heat exchanger 420 can be at least 50% steam (vaporous cryogen quality/liquid refrigerant quality).Also can make system's 400 work that the refrigerant vapour surge of at least 75% or at least 90% steam is provided with the start-up portion to external heat exchanger 420.These surges can make peak temperature at intermittence that the start-up portion of evaporimeter reaches be in below the low approximately temperature of 5 ℃ of temperature than the second foreign medium 460.The peak temperature at intermittence that the start-up portion of evaporimeter reaches also can be in than below the low approximately temperature of 2.5 ℃ of the temperature of the second foreign medium 460.These intermittently peak temperature preferably higher than the dew point of outdoor air.Also can reach other intermittently peak temperatures.
When working with heating mode as shown in Figure 4 B, system 400 also can work provides approximately 1.9Kcal with the start-up portion from external heat exchanger 420 to exit portion thh -1m -2℃ -1～about 4.4Kcal thh -1m -2℃ -1Mean heat transfer coefficient.Mean heat transfer coefficient is by measuring heat transfer coefficient from starting point at least 5 points to terminal of external heat exchanger coil pipe and the coefficient of gained being averaged to determine.This heat transfer property of system 400 is with respect to the non-surge formula of the tradition heat pump part that significantly improves, and in the non-surge formula of tradition heat pump, the start-up portion of the external heat exchanger externally initial part office of heat exchanger coils has lower than about 1.9Kcal thh -1m -2℃ -1Heat transfer coefficient, the external heat exchanger part before outlet in have lower than about 0.5Kcal thh -1m -2℃ -1Heat transfer coefficient.
Although system 400 is sent to heat with the efficient larger than legacy system 200 and is conditioned the space, also must consider another factor, namely provide to the temperature of the air that is conditioned the space.For example, will make the room be warming up to the temperature of expectation although relative humidity (RH) is 45% the air of 31 ℃, dermal sensation is got up not warm.Thereby, can increase defrosting and hot extraction efficiency although make external heat exchanger 420 compare the conventional heat pump system with the surge work pattern, the air that system 400 may not produce within specific time period after enough heats make heating reaches the temperature of feeling warm when being conditioned the space offering.For example, if can transmitting enough heats, system 400 make air themperature raise approximately 35 ℃, the outdoor temperature of-10 ℃ will make provide to the air that is conditioned the space be 25 ℃, and the outdoor temperature of 5 ℃ will make provide to the air that is conditioned the space be 40 ℃.Although both all can heat to acceptable level being conditioned the space, it is warm that the air of 40 ℃ will be felt, and the air of 27 ℃ can not.Usually, it is believed that temperature is that approximately 50 ℃ and above air " feel enough warm ".
If use optional Flow-rate adjustment member 432, always can produce extra heat at internal exchanger 440 places, but because extra wearing and tearing can occur and cause thus energy loss on compressor 410, may not wish that the cold-producing medium that depends on by limiting from indoor heat exchanger 440 flows the higher pressure that produces.Although very common in the conventional heat pump system, compressor is overcome produce than the upper larger load operation of required load of operation extra " frictional heat " be very poor efficiency can.Similarly, compare the larger compressor of the refrigeration needed compressor of script by use and also can produce extra heat, however the efficient of can losing the job equally.
Thereby, although system 400 can make from the outside to inner heat transfer efficiency and maximize, useful is is sent to extra heat internal exchanger 440 on time per unit during heating provide not only can heat and be conditioned the space but also feel warm air.Although system 400 can use one or more restrictions (for example the Flow-rate adjustment member 432) that extra heat was provided on the unit interval, but produce the working life that frictional heat can shorten compressor 410, and for being poor efficiency for the heat of outdoor transmission.
With sensor 422 monitor temperatures and/or pressure in a kind of mode that additional heat is provided to internal exchanger 440 on time per unit before the outlet of externally heat exchanger 420.In this way, can reduce flow to metering device 433 transmitted signals, thereby the surge operation of evaporimeter is reduced to sensor 422 evaporator section before.Although sensor 422 is positioned at half place of pact of the coil pipe of external heat exchanger 420, sensor 422 also can be positioned at any position before outlet with external heat exchanger 420 outsides of the expectation work compatibility of system 400.For example, sensor 422 also can be placed to apart from about 1/3rd or 2/3rds places of the entrance of external heat exchanger 420.Be placed on 1/3rd places and will make approximately 1/3rd evaporimeter with the surge work pattern, will make approximately 2/3rds evaporimeter with the surge work pattern and be placed on 2/3rds places.
When metering device 433 during in response to sensor 422 rather than sensor 421, because external heat exchanger 420 is not that whole volume is all with surge work pattern (remaining coil pipe is with overheated work pattern basically), so from outdoor Efficiency Decreasing to being conditioned the space and conducting heat.Yet in this pattern (the outdoor evaporator operation of part surge), due to the superheat section of evaporimeter, time per unit can be sent to internal exchanger 440 with more heat.This superheat section of evaporimeter makes can and feel that with higher temperature warmer air provides to being conditioned the space.
Which in two sensors 421 of choice for use, 422 controlling metering device 433 by during heating, system 400 can switch between high heat transfer efficiency pattern and higher temperature pattern.By part surge and the overheated evaporator operation of part, system 400 is worked under the higher temperature pattern, this can reduce or eliminate the needs of the extra friction heat that is produced in response to Flow-rate adjustment member 432 by compressor.In addition, if Flow-rate adjustment member 432 allows to regulate during operation, system 400 can work or work under the higher temperature pattern under high heat transfer efficiency pattern, wherein, extra heat recently obtains from the frictional heat that increases (realizing by adjust flux adjustment means 432) and/or the percentage that operates by the surge that reduces in external heat exchanger 420.
Fig. 5 A (refrigeration) and Fig. 5 B (heating) expression have the surge formula refrigeration of independent complete surge circuit and part surge circuit and heat heat pump 500.Although an external heat exchanger 520 is shown, surge circuit and part surge circuit also can use independent evaporimeter fully.In some cases, when using single phase separator, measurement mechanism and evaporimeter, possibly can't realize complete surge operation and the operation of part surge both.Even in the time can realizing, may wish that also optimizing each circuit realizes maximum performance, and described maximum performance possibly can't realize when using single Circuits System (as system 300).
The element that comprises system 300, system 500 has increased extra phase separator 525 and extra metering device 526.Sensor 521 is controlled metering device 533, so that the surge operation to be provided in all external heat exchanger 520.Similarly, sensor 522 is controlled metering device 526, externally to provide the operation of part surge in heat exchanger 520.Can at any time control which surge circuit with the switch valve 523 and 524 of electric means control works.If metering device 526,533 can turn-off respectively cold-producing medium stream basically, valve 523,524 can omit.Can programme to determine when (Fig. 5 B) opens valve 523 during heating the higher temperature pattern of part surge formula is provided or opens the high heat transfer efficiency pattern that valve 524 provides complete surge formula to controller 580.If metering device 526,533 can be turned off cold-producing medium stream basically, can control to select required mode of operation to them by controller 580.
If during freezing (Fig. 5 A) with phase separator 525,534, metering device 526,533 or valve 523,524 in one or more bypass of advantageously carrying out, system 500 can be provided with in optional bypass circulation 572 and one way stop peturn valve 573 and Flow-rate adjustment member 574 one or both.Therefore, if any one device backflow refrigerant effectively during freezing in these devices can be carried out bypass to it.But use traffic adjustment means 574 is optimized the high-pressure refrigerant stream that flows to metering device 530 during freezing.Such as before for system 300 and system 400 discussion, system 500 can be equipped with bypass circulation 571, one way stop peturn valve 570 and Flow-rate adjustment member 532 selectively, during heating, metering device 530 and phase separator 531 are carried out bypass.If Flow-rate adjustment member 532 is automatically controlled, controller 590 can change must work restriction to overcome of compressor 510 during heating, and provides to the temperature of the air that is conditioned the space with rising.Therefore, controller 590 can to valve 523,524 and Flow-rate adjustment member 532 control, thereby realize heat transfer efficiency and provide to the desired balance between the air themperature that is conditioned the space.System 500 can have element still less or also have extra element.
Fig. 6 represents the flow chart be used to the method 600 that operates the heat pump that comprises at least one phase separator as above.In step 602, cold-producing medium is compressed.In step 604, cold-producing medium is expanded.In step 606, separate at least in part liquid phase and the gas phase of cold-producing medium.In step 808, one or more surges of the gas phase of cold-producing medium are introduced in the start-up portion of evaporimeter.A plurality of surges of the gas phase of cold-producing medium can comprise at least 75% steam.The start-up portion of evaporimeter can be less than approximately 10% or less than approximately 30% of evaporimeter volume of evaporimeter volume.Start-up portion can have other volumes of evaporimeter.In step 610, the liquid phase of cold-producing medium is introduced in evaporimeter.
In step 612, in response to the start-up portion of one or more surge heating fumigators of the gas phase of cold-producing medium.The start-up portion of evaporimeter can be heated to less than the low approximately temperature of 5 ℃ of temperature than the first foreign medium or the second foreign medium.The start-up portion of evaporimeter can be heated above the temperature of the first foreign medium or the second foreign medium.The start-up portion of evaporimeter can be heated above the temperature of the dew-point temperature of the first foreign medium or the second foreign medium.Temperature difference between evaporator inlet volume and outlet volume can be approximately 0 ℃～approximately 3 ℃.Can operate heat pump, make slope in the temperature of the start-up portion of evaporimeter comprise negative value and on the occasion of.The start-up portion of evaporimeter can distil or melt frost.When the temperature of the start-up portion of evaporimeter was equal to or less than approximately 0 ℃, frost can distil.
Fig. 7 represents the flow chart for the method 700 that the evaporimeter that comprises the heat pump of at least one phase separator as above is defrosted.In step 702, separate at least in part liquid phase and the gas phase of cold-producing medium.In step 704, one or more surges of the gas phase of cold-producing medium are introduced in the start-up portion of evaporimeter.A plurality of surges of the gas phase of cold-producing medium can comprise at least 75% steam.The start-up portion of evaporimeter can be less than approximately 10% or less than approximately 30% of evaporimeter volume of evaporimeter volume.Start-up portion can have other volumes of evaporimeter.In step 906, the liquid phase of cold-producing medium is introduced in evaporimeter.
In step 708, in response to the start-up portion of one or more surge heating fumigators of the gas phase of cold-producing medium.The start-up portion of evaporimeter can be heated to less than the low approximately temperature of 5 ℃ of temperature than the first foreign medium or the second foreign medium.The start-up portion of evaporimeter can be heated above the temperature of the first foreign medium or the second foreign medium.The start-up portion of evaporimeter can be heated above the temperature of the dew-point temperature of the first foreign medium or the second foreign medium.Temperature difference between evaporator inlet volume and outlet volume can be approximately 0 ℃～approximately 3 ℃.Can operate heat pump, make the slope of temperature of the start-up portion of evaporimeter comprise negative value and on the occasion of.
In step 710, from evaporator defrost.Defrosting comprises preventing frosting basically.Defrosting comprises the existence of basically eliminating frost from evaporimeter.Defrosting comprises to be eliminated frost from evaporator section ground or fully.The start-up portion of evaporimeter can distil or melt frost.When the temperature of the start-up portion of evaporimeter was equal to or less than approximately 0 ℃, frost can distil.
Fig. 8 represents for phase separator being added the flow chart of bypass with the method 800 of carrying out heating operation.In step 810, insert bypass circulation, with between the point after the point before metering device and the phase separator that is associated but set up cold-producing medium and flow before internal exchanger.In step 820, one way stop peturn valve and Flow-rate adjustment member are inserted in bypass circulation.Preferably, set the Flow-rate adjustment member, make it provide minimum restriction to cold-producing medium stream.In step 830, the temperature difference between the air of determining to enter the air of internal exchanger and leave internal exchanger.In step 840, in response to described temperature difference adjust flux adjustment means, to reduce the cold-producing medium stream of the Flow-rate adjustment member of flowing through during heating, keep simultaneously required amperage and the running parameter of compressor.Can increase other elements and carry out other adjustment in system, so that required efficient and air pressure to be provided.
For example, and usually according to the system of Fig. 2 B, the conventional heat pump system is assembled by steam compressed unit and internal exchanger.The model of steam compressed unit is that HP29-0361P, sequence number are 5801D6259, and comprises compressor, external heat exchanger, blower fan and relevant control piece.Compressor is single-phase, and it is 208 volts or 230 volts that load rated safety uses voltage, and the maximum recommended current drain is 21.1 amperes.The model of internal exchanger is C23-46-1, and sequence number is 6000K1267.When this system approximately 208 volts sentence heating mode when work, compressor consumes approximately 16.8 amperes, provides the approximately air of 55.5 ℃ to being conditioned the space simultaneously under the external air temperature of approximately-9.4 ℃.System held approximately 23 ℃ be conditioned the space air themperature.
This conventional heat pump system improves with two phase separators, to provide the surge operation to internal exchanger and external heat exchanger.This improvement is carried out according to Fig. 4 B usually, but omits bypass circulation, one way stop peturn valve and the Flow-rate adjustment member that the phase separator of surge operation is provided to internal exchanger.When this with phase separator improved system at approximately 208 volts when sentencing heating mode work, compressor consumes approximately 12.4 amperes, provides the approximately air of 32.2 ℃ to being conditioned the space simultaneously under the external air temperature of approximately-9.4 ℃.System held approximately 23 ℃ be conditioned the space air themperature.Therefore, although compare with legacy system to being conditioned the space and providing the air of lower temperature (approximately 32 ℃ vs. approximately 55 ℃), with the improved system held of phase separator approximately the expectation of 23 ℃ be conditioned the space air themperature.This high heat transfer efficiency heat mode of operation with current drain from approximately 17 amperes be reduced to approximately 12 amperes, current drain has reduced approximately 30% (17-12/17*100), still keeping approximately simultaneously, the expectation of 23 ℃ is conditioned space temperature.Therefore, have during heating to external heat exchanger and provide the system of the phase separator of surge operation to heat to the temperature of expectation, the electric current that obviously lacks than the conventional heat pump system consumption simultaneously being conditioned the space.
Then, according to method 800 and usually according to the system of Fig. 4 B, the subtend internal exchanger provides the phase separator of surge operation to carry out bypass.Therefore, the phase separator that provides surge operation to internal exchanger is by bypass, and provides the phase separator of surge operation not by bypass to external heat exchanger.System after improving with this bypass phase separator approximately 208 volts sentence heating mode when work, compressor consumes approximately 15.9 amperes, provides the approximately air of 60 ℃ to being conditioned the space simultaneously under the external air temperature of approximately-9.4 ℃.System held approximately 23 ℃ be conditioned the space air themperature.Therefore, compare with legacy system, the system after improving with the bypass phase separator provides air with higher temperature (approximately 60 ℃ vs. approximately 55 ℃) to being conditioned the space, and keeps approximately that the expectation of 23 ℃ is conditioned the space air themperature.This higher temperature heat mode of operation with current drain from approximately 17 amperes be reduced to approximately 16 amperes (having reduced approximately 6% (17-16/17*100)), making simultaneously provides to the temperature of the air that is conditioned the space approximately 8% (60-55.5/55.5*100) that raise.Therefore, system compares with conventional heat pump, and having to internal exchanger and external heat exchanger provides the surge operation and can provide the air of higher temperature to being conditioned the space heating the system of duration of work with the phase separator of bypass, draws simultaneously electric current still less.

Claims (56)

1. method that operates heat pump, it comprises:
Cold-producing medium is compressed;
Described cold-producing medium is expanded;
Liquid phase and the gas phase of separating at least in part described cold-producing medium;
At least one surge of the described gas phase of described cold-producing medium is introduced in the start-up portion of internal exchanger;
The described liquid phase of described cold-producing medium is introduced in described internal exchanger;
In response to described at least one surge of the described gas phase of described cold-producing medium and heat the described start-up portion of described internal exchanger;
Make the flow inversion of described cold-producing medium;
The described cold-producing medium that expands is introduced in external heat exchanger.
2. the method for claim 1, it also comprises: the described start-up portion of described internal exchanger is heated to the low approximately temperature of 5 ℃ of temperature than the first foreign medium at the most.
3. the method for claim 1, it also comprises: the temperature that the described start-up portion of described internal exchanger is heated above the first foreign medium.
4. the method for claim 1, it also comprises: the described start-up portion of described internal exchanger is heated to the temperature higher than the dew-point temperature of the first foreign medium.
5. the method for claim 1, wherein during freezing, the temperature difference between the entrance volume of described internal exchanger and the outlet volume of described internal exchanger is approximately 0 ℃～approximately 3 ℃.
6. the method for claim 1, it also comprises: operating said system, the slope of the temperature of the described start-up portion of wherein said internal exchanger comprise negative value and on the occasion of.
7. the method for claim 1, it also comprises: from the described start-up portion defrosting of described internal exchanger.
8. the method for claim 1, it also comprises: make frost from the described start-up portion distillation of described evaporimeter, the temperature of the described start-up portion of wherein said internal exchanger is approximately 0 ℃ at the most.
The method of claim 1, wherein the described start-up portion of described internal exchanger less than approximately 30% of the volume of described internal exchanger.
The method of claim 1, wherein the described start-up portion of described internal exchanger less than approximately 10% of the volume of described internal exchanger.
11. the method for claim 1, wherein
The described start-up portion of described internal exchanger has at least one batch temperature maximum, and
Described at least one batch temperature maximum is in response to described at least one surge of the described gas phase of described cold-producing medium, and
Described batch temperature maximum is in than below the low approximately temperature of 5 ℃ of the temperature of the first foreign medium.
12. method as claimed in claim 11, wherein, described at least one batch temperature maximum is higher than the temperature of described the first foreign medium.
13. method as claimed in claim 11, wherein, described at least one batch temperature maximum is higher than the dew-point temperature of described the first foreign medium.
14. method as claimed in claim 11, wherein, the volume of front 10% and described evaporimeter of the volume of described internal exchanger rear 10% between temperature difference be approximately 0 ℃～approximately 3 ℃.
15. method as claimed in claim 11, wherein, the relative humidity of described the first foreign medium is greater than the relative humidity of described the first foreign medium when not introducing the surge of described vapor phase refrigerant to the described start-up portion of described internal exchanger.
16. method as claimed in claim 11, wherein, the temperature of described the first foreign medium is lower than the temperature of described the first foreign medium when not introducing the surge of described vapor phase refrigerant and using the active defrosting cycle to the described start-up portion of described internal exchanger.
17. method as claimed in claim 11, it also comprises: operating said system, the slope of the temperature of the described start-up portion of wherein said internal exchanger comprise negative value and on the occasion of.
18. method as claimed in claim 11, it also comprises: the described start-up portion in response to described batch temperature maximum from described internal exchanger defrosts.
19. method as claimed in claim 11, it also comprises: in response to described batch temperature maximum, make frost from the described start-up portion distillation of described internal exchanger, the temperature of the described start-up portion of wherein said internal exchanger is approximately 0 ℃ at the most.
20. method as claimed in claim 11, wherein, the described start-up portion of described internal exchanger is less than approximately 30% of the volume of described internal exchanger.
21. method as claimed in claim 11, wherein, the described start-up portion of described internal exchanger is less than approximately 10% of the volume of described internal exchanger.
22. the method for claim 1, wherein described at least one surge of the described gas phase of described cold-producing medium comprises at least 75% steam.
23. the method for claim 1, wherein the mean heat transfer coefficient from the described start-up portion of described internal exchanger to exit portion is about 1.9Kcal thh -1m -2° C -1～about 4.4Kcal thh -1m -2° C -1, and wherein,
The described start-up portion of described internal exchanger is less than approximately 10% of the volume of described internal exchanger, and wherein
The described exit portion of described internal exchanger is less than approximately 10% of the volume of described internal exchanger.
24. the method for claim 1, it also comprises:
The mobile of cold-producing medium that leaves described internal exchanger limited; And
Produce frictional heat in response to described restriction.
25. method as described in claim 1 or 24, it also comprises: at least one surge of the described gas phase of described cold-producing medium is introduced in the start-up portion of described external heat exchanger, the described liquid phase of described cold-producing medium is introduced in described external heat exchanger, and in response to described at least one surge of the described gas phase of described cold-producing medium and heat the described start-up portion of described external heat exchanger.
26. method as claimed in claim 25, wherein, the described cold-producing medium that leaves described external heat exchanger comprises liquid phase.
27. method as claimed in claim 25, wherein, the described cold-producing medium that leaves described external heat exchanger does not have liquid phase.
28. one kind to the method that is conditioned the space or from be conditioned the space diabatic process, the evaporimeter of heat pump is defrosted, it comprises:
Liquid phase and the gas phase of separating at least in part cold-producing medium;
At least one surge of the described gas phase of described cold-producing medium is introduced in the start-up portion of described evaporimeter;
The described liquid phase of described cold-producing medium is introduced in described evaporimeter;
In response to described at least one surge of the described gas phase of described cold-producing medium, the described start-up portion of the described evaporimeter of heating; And
From described evaporator defrost.
29. method as claimed in claim 28, it also comprises: the described start-up portion of described evaporimeter is heated to hang down the approximately temperature of 5 ℃ than the temperature of the first foreign medium or the second foreign medium at the most.
30. method as claimed in claim 28, it also comprises: the temperature that the described start-up portion of described evaporimeter is heated above the first foreign medium or the second foreign medium.
31. method as claimed in claim 28, it also comprises: the described start-up portion of described evaporimeter is heated to the high temperature of dew-point temperature than the first foreign medium or the second foreign medium.
32. method as claimed in claim 28, wherein, the temperature difference between the entrance volume of described evaporimeter and the outlet volume of described evaporimeter is approximately 0 ℃～approximately 3 ℃.
33. method as claimed in claim 28, wherein, the slope of the temperature of the described start-up portion of described evaporimeter comprise negative value and on the occasion of.
34. method as claimed in claim 28, it also comprises: make frost from the described start-up portion distillation of described evaporimeter.
35. method as claimed in claim 28, it also comprises: make frost from the described start-up portion distillation of described evaporimeter, the temperature of the described start-up portion of wherein said evaporimeter is approximately 0 ℃ at the most.
36. method as claimed in claim 28, wherein, the described start-up portion of described evaporimeter is less than approximately 30% of the volume of described evaporimeter.
37. method as claimed in claim 28, wherein, the described start-up portion of described evaporimeter is less than approximately 10% of the volume of described evaporimeter.
38. method as claimed in claim 28, wherein, described at least one surge comprises at least 75% steam.
39. a heat pump, it comprises:
Compressor, it has entrance and outlet, and described entrance and described outlet are communicated with flow inversion device fluid;
External heat exchanger, it has entrance and outlet;
Internal exchanger, it has entrance, start-up portion, further part and outlet, the described outlet of described compressor is communicated with the described inlet fluid of described external heat exchanger, the described outlet of described external heat exchanger is communicated with the described inlet fluid of described internal exchanger, and the described outlet of described internal exchanger is communicated with the described inlet fluid of described compressor;
The first metering device, it is communicated with described external heat exchanger and described internal exchanger fluid, and wherein said the first metering device expands cold-producing medium and enters in described internal exchanger, and described cold-producing medium has steam part and liquid part;
The first-phase separator, it is communicated with described the first metering device and described internal exchanger fluid,
Wherein, described first-phase separator is operable as a part that makes described steam to be separated with the described cold-producing medium of expansion, and wherein
At least one surge that described first-phase separator is operable as described steam is introduced in the described start-up portion of described internal exchanger;
The second metering device, it is communicated with described external heat exchanger and described internal exchanger fluid, and wherein said the second metering device expands described cold-producing medium and enters in described external heat exchanger.
40. system as claimed in claim 39, wherein, described first-phase separator has body, and described body defines separator inlet, separator outlet and separator refrigerant storage chambers;
Wherein, described separator refrigerant storage chambers has longitudinal size;
Wherein, the diameter of described separator inlet is approximately 1:1.4～4.3 or approximately 1:1.4～2.1 to the ratio of the diameter of described separator outlet; And
Wherein, the described diameter of described separator inlet is about 1:7～13 to the ratio of described longitudinal size.
41. system as claimed in claim 40, wherein, the described diameter of described separator inlet is 1:1～12 to the ratio of refrigerant mass fluxes.
42. system as claimed in claim 39, wherein, described at least one surge is from the described start-up portion defrosting of described internal exchanger.
43. system as claimed in claim 39, wherein, described at least one surge makes frost from the described start-up portion distillation of described internal exchanger, approximately 0 ℃ at the most of the temperature of the described start-up portion of described internal exchanger.
44. system as claimed in claim 39, wherein, described first-phase separator is operable as the described start-up portion that two surges of described steam is introduced into described internal exchanger in the operation cycle of described compressor at least.
45. system as claimed in claim 39, wherein, the described start-up portion of described internal exchanger be described internal exchanger cumulative volume at the most 30%.
46. system as claimed in claim 39, wherein, the described start-up portion of described internal exchanger be described internal exchanger cumulative volume at the most 10%.
47. system as claimed in claim 39, wherein, described at least one the steam surge that is introduced into the described start-up portion of described internal exchanger makes the described start-up portion of described internal exchanger be increased at least one batch temperature maximum, and described at least one batch temperature maximum is in than below the low approximately temperature of 5 ℃ of the temperature of the first foreign medium.
48. system as claimed in claim 39, wherein, described at least one the steam surge that is introduced into the described start-up portion of described internal exchanger makes the described start-up portion of described internal exchanger be increased at least one batch temperature maximum, and described at least one batch temperature maximum is higher than the temperature of the first foreign medium.
49. system as claimed in claim 39, wherein, described at least one the steam surge that is introduced into the described start-up portion of described internal exchanger makes the described start-up portion of described internal exchanger be increased at least one batch temperature maximum, and described at least one batch temperature maximum is higher than the dew-point temperature of the first foreign medium.
50. system as claimed in claim 39, wherein, the volume of front 10% and described evaporimeter of the volume of described internal exchanger rear 10% between temperature difference be 0 ℃～3 ℃.
51. system as claimed in claim 39, wherein, described at least one surge comprises at least 75% steam.
52. system as claimed in claim 39, it also comprises the first flow adjustment means that is communicated with described internal exchanger and described the second metering device fluid.
53. system as described in claim 39 or 52, it also comprises the second-phase separator that is communicated with described the second metering device and described external heat exchanger fluid.
54. system as described in claim 39 or 52, it also comprises the second-phase separator that is communicated with described the second metering device and described external heat exchanger fluid and the 3rd metering device that is communicated with described external heat exchanger and described internal exchanger fluid, wherein, described the 3rd metering device expands described cold-producing medium and enters the third phase separator, and described third phase separator is communicated with described the 3rd metering device and described external heat exchanger fluid.
55. system as claimed in claim 54, it also comprises the second flow adjustment means that is communicated with described external heat exchanger and described the first metering device fluid.
56. one kind arranges bypass to heat the method for operation at least one phase separator, described method comprises:
Insert bypass circulation, with between the point after the point before metering device and the phase separator that is associated but set up cold-producing medium and flow before internal exchanger;
One way stop peturn valve and Flow-rate adjustment member are inserted in described bypass circulation;
Temperature difference between the air of determining to enter the air of described internal exchanger and leave described internal exchanger; And
Regulate described Flow-rate adjustment member in response to described temperature difference, to reduce the described cold-producing medium stream of the described Flow-rate adjustment member of flowing through during heating, keep simultaneously for required amperage and the running parameter of the compressor of cold-producing medium are provided to described Flow-rate adjustment member.
CN201180036993.2A 2010-05-27 2011-05-27 Surge formula heat pump Expired - Fee Related CN103180678B (en)

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US9057547B2 (en) 2015-06-16
US20170074565A1 (en) 2017-03-16
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US10060662B2 (en) 2018-08-28
US20130174589A1 (en) 2013-07-11
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AU2011258052A1 (en) 2013-01-10
US9879899B2 (en) 2018-01-30

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